CN102959051B - Improved heat pump distillation for <50% light component in feed - Google Patents
Improved heat pump distillation for <50% light component in feed Download PDFInfo
- Publication number
- CN102959051B CN102959051B CN201180029142.5A CN201180029142A CN102959051B CN 102959051 B CN102959051 B CN 102959051B CN 201180029142 A CN201180029142 A CN 201180029142A CN 102959051 B CN102959051 B CN 102959051B
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- China
- Prior art keywords
- stream
- side discharging
- rectifying section
- compression
- make
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
A process is presented for the separation of a hydrocarbon mixture having less than 50% of the light component in the feedstream. The process provides an energy efficiency through drawing off a vapor stream from the rectifying section of a distillation column, and using recompression of the vapor to provide a portion of the heat for reboiling a portion of the bottoms stream exiting the stripping section of the distillation column.
Description
Right of priority statement
The application requires the U. S. application No.61/359 submitting on June 30th, 2010,869 right of priority.
Invention field
Field of the present invention relates to the separation of hydrocarbon.Particularly, the present invention relates to improve the energy use of the hydrocarbon component for there is approximate boiling point by fractionation by distillation.
Background of invention
The separation of hydrocarbon is the basic skills in petroleum industry.Oil is the mixture of many hydrocarbon compounds, by compound separation and for different objects, and the such as raw material of fuel, lubricant, polymeric device etc.A kind of separation method in petroleum industry is distillation.Distillation is the different of relative volatility based on each component in mixture and the different separation method that therefore forms between liquid mixture and the steam being formed by liquid mixture.In the standard continuous distillation method that comprises multiple stages, the difference of composition allows that the part in each stage separates.Liquid phase and vapor phase were entered in the different stages, and further generation have different new liquid phase and the vapor phases that form separately.Standard Distallation systm comprises high tower, and steam upwards flows and contacts with the liquid flowing downward.Vapor phase by adding enough heat so that liquid seethes with excitement or evaporates in the time reaching tower bottom forms, and steam condensation in the time leaving top of tower.The method expends large energy to process continuously hydrocarbon flow, and conventionally uses multiple towers incoming flow is separated into multiple product streams.
The problem of Distallation systm is that they are large users of energy and energy is used and to consume efficiency low.The improvement of design can significantly reduce energy expenditure.Reduce the CO relevant with energy expenditure along with improving cost of energy with improving
2the pressure of discharge, in the urgent need to more effective distillation design.
Summary of the invention
Energy efficiency is important for energy-intensive process.With fractionation by distillation hydrocarbon compound be energy-intensive, and separate and there is the hydrocarbon compound of the component that approaches boiling point, energy is significant.The invention provides the hydrocarbon separation that improves energy efficiency.The present invention is the method for separation of lighter component from hydrocarbon mixture.Make the position of hydrocarbon incoming flow between rectifying section and stripping stage enter distillation tower, and wherein incoming flow comprise and have the mixture that is less than 50% light component.Distillation tower has overhead vapor stream, and this overhead vapor stream enters in the first heat pump compressor, produces the overhead vapor stream of compression.The steam side that the overhead vapor stream of compression enters the first reboiler interchanger.By the overhead vapor stream condensation at least in part of compression.Distillation tower has bottom stream, and first part's bottom stream enters the hydraulic fluid side of the first reboiler interchanger, and evaporation at least partly.Steam returns to distillation tower.The present invention further comprises side steam flow is taken out from rectifying section at discharge port, produces thus side discharging stream.Side discharging flows to into the second heat pump compressor, produces the side discharging stream of compression.The side discharging of compression flows to the steam side into the second reboiler interchanger, produces cooling side discharging stream.Second section bottom stream enters the hydraulic fluid side of the second reboiler interchanger, there second section is evaporated at least partly.Steam from the second section of the second interchanger returns to distillation tower, and cooling side discharging stream returns to the rectifying section of distillation tower.
In one embodiment, side discharging stream is taken out from lower part of the rectifying section of distillation tower.
Other object of the present invention, embodiment and details can be obtained by the following drawings and detailed Description Of The Invention.
Accompanying drawing summary
Fig. 1 is for reducing the schematic diagram of heat pump that approaches the energy requirement in the separation of boiling point liquid.
Fig. 2 shows as the thermograde on the distillation tower of the function of stage number.
Fig. 3 shows that the temperature of propane-propylene separation tower is with respect to the tower total composite curve of enthalpy.
Fig. 4 shows that the number of stages of propane-propylene separation tower is with respect to the tower total composite curve of enthalpy.
Detailed Description Of The Invention
The problem that hydrocarbon compound separates is that to have the compound that approaches boiling point be height energy-intensive.Distillation is the most popular method of hydrocarbon liquid separating composition being opened to component.This is generally used for having the liquid of narrower composition, but also can be used for each relatively pure component of preparation.Distillation is also unusual energy-intensive, and relates to the fuel cost of annual multi-million dollar.Can use heat pump or mechanical steam to recompress to reduce these cost of energy.Heat pump effectively uses the energy of steam machinery recompression and the energy calorimetric in steam is transferred to another fluid.This means heat energy and is transferred to liquid by compressed vapour, wherein partially or completely condensation of liquid boiling and compressed vapour.This is true especially to approaching the separation of boiling point component in hydrocarbon mixture.Any improvement that reduces energy intensity can affect economy prepared by many hydrocarbon compounds significantly.
The present invention is intended to separation of lighter component from hydrocarbon mixture.Charging therein comprises in the situation that is less than 50 % by weight light component, and overhead vapor stream can be used for heat to be transferred to individually reboiler.But, by taking out side discharging stream, there is lower compression ratio, therefore less mechanical energy promotes side discharging to the second reboiler temperature, improves thus the efficiency of tower.Fig. 1 is the elaboration of novel method.The method comprises that making to have the position 22 of the incoming flow 10 that is less than 50% light component between rectifying section 24 and stripping stage 26 enters distillation tower 20.Distillation tower produces overhead vapor stream 28 and bottom liquid stream 30.Light component is the required component separating from hydrocarbon mixture, is recovered in overhead vapor stream.
Overhead vapor stream 28 enters in the first heat pump compressor 40 to produce the overhead vapor stream 42 of compression.The steam side that the overhead vapor stream of compression enters the first reboiler interchanger 44, there by cooling the overhead vapor stream of compression and at least part of condensation 46.Preferably, operation the method is with the overhead vapor stream of total condensation compression.The top of compression steam flow of part condensation returns to the top of rectifying section as backflow.First part's bottom liquid stream 32 enters the hydraulic fluid side of the first reboiler interchanger 44.First part 32 is flashed to steam flow 34 and return to the bottom of the stripping stage 26 of distillation tower 20.The top that the overhead 46 of a part 48 condensations enters rectifying section 24 as backflow is for distillating method.
The method further comprises takes out steam effluent from rectifying section 24, produces side discharging stream 52, and it is taken out from side discharge port 53.Side discharging stream 52 compression in the second heat pump compressor 50 is flowed to 54 with the side discharging that produces compression.The side discharging stream 54 steam sides that enter the second reboiler interchanger 60 of compression, produce cooling compressed side discharging stream 56.Cooling side discharging stream 56 returns to the rectifying section 24 of distillation tower 20.Can be by cooling compressed side discharging stream 56 partially or completely condensations.In one embodiment, rectifying section is returned near the position that cooling side discharging is flowed side discharge port 53.In one embodiment, side discharging stream 56 cooling and at least part of condensation enters the position of side discharge port below 53 in rectifying section 24.
Second section 36 bottom liquid stream enter the hydraulic fluid side of the second reboiler interchanger 60.Second section 36 is heated to vapor phase 38 and enters the bottom of the stripping stage 26 of distillation tower 10.
The optimum position of side discharge port 53 is positioned at apart from the column plate place of 10 column plates of column plate with larger thermograde in rectifying section 24.Temperature gradient curve about propane-propylene separation tower is shown in Fig. 2.In one embodiment, side discharge port 53 is arranged in the rectifying section 24 and the immediate column plate of the column plate place with maximum temperature gradient of tower 20.In another embodiment, side discharge port 53 is arranged in the column plate place of rectifying section 24 lower parts.
Steam flow to reboiler can be brought the energy from steam in reboiler into.Flow process can separate steam discharging, and some are sent to side discharging.Side discharging has less compression ratio requirement, therefore can have some saving compared with the compression of only rectifying overhead vapor compression.
Simulation is used the calorifics force data operation of propane and propylene.Charging comprises 35% propylene, and nominal operation pressure is 170psia (1172kPa).The feeding temperature of distillation tower ingress is 87 ℉ (30.6 DEG C).For having the tower of 160 column plates, feed tray is 114 grades (stage), or theoretical tray 114, the column plate that wherein the first column plate is top.Rectifying section 24 comprises column plate 1-113, and stripping stage 26 comprises column plate 115-160.Term column plate and theoretical stage are interchangeable with regard to this discussion about distillation tower.
Distillation tower has along the thermograde of tower height degree, and about the example of propane-propylene separation tower, this can be referring to Fig. 2.Distillation tower also has tower total composite curve (CGCC), and this curve display goes out the temperature as the function of enthalpy loss (enthalpy deficit), as shown in Figure 3.This also can be shown as tower level or theoretical tray as the function of enthalpy loss.In Fig. 3, enthalpy loss curve has two portions: first or top of curve shows the enthalpy loss in distillation exhausting section of column 26; Enthalpy loss in the rectifying section 24 of second or the bottom demonstration distillation tower of curve.Enthalpy loss derives from and causes in lack of balance system the entropy effect of waste of energy on border.When charging comprises while being less than 50% lighting end, the position of discharging stream is in rectifying section, and the speed of temperature variation is larger as the function of the enthalpy loss of rectifying section there.
Enthalpy loss can be drawn with respect to the level position in distillation tower, as shown in Figure 4.In the time searching out the suitable tower of discharge port position, optimum position is near the curve in the time that enthalpy loss turns to respect to progression.In this simulation, optimum position is near column plate or theoretical stage 80.
Another simulation is carried out about the several towers not at the same level that have of the typical commercial operation for propylene preparation.This simulation is for the production of the commercial apparatus of 500kMTA.Propylene and separating of propane are unusual energy-intensive, and interpolation equipment can easily be offset by the saving of cost of energy.The analog result with the tower of 160 theoretical stages is shown in following table.Basic condition is the standard set-up without side discharge port or heat pump reboiler, and has the situation of heat pump reboiler or inter-stage reboiler.
Table: expense contrast
This simulation shows the payback period with about 13 months, and significant operation is saved.These are simulated all for identical product purity, and wherein propylene product stream has 99.5% purity.Energy saving is along with product purity improves and improves.
Although described the present invention about the preferred embodiment of thinking at present, be to be understood that and the invention is not restricted to disclosed embodiment, but it is intended to contain the various improvement and the equivalent that are included in claims scope.
Claims (7)
1. the method for separation of lighter component from hydrocarbon mixture, it comprises:
Make the position of incoming flow between rectifying section and stripping stage enter distillation tower, wherein charging comprises the light component that is less than 50%, and wherein distillation tower has overhead vapor stream and bottom liquid stream;
Make overhead vapor stream enter the first heat pump compressor, produce thus the overhead vapor stream of compression;
The steam side that makes the overhead vapor stream of compression enter the first reboiler interchanger, produces the overhead of whole condensations thus;
Make the overhead of a part of condensation enter the top of rectifying section,
At discharge port, side steam flow is taken out from rectifying section, produce thus side discharging stream, wherein side discharging stream is arranged in apart from the column plate of 10 column plates of column plate with the every column plate of maximum temperature gradient and is taken out from rectifying section;
Side discharging is flow to into the second heat pump compressor, produce thus the side discharging stream of compression;
Make the side discharging of compression flow to the steam side into the second reboiler interchanger, produce thus cooling compressed side discharging stream;
Make first part's bottom liquid stream enter the hydraulic fluid side of the first reboiler interchanger, produce thus the first steam bottom stream; With
Make second section bottom liquid stream enter the hydraulic fluid side of the second reboiler interchanger.
2. according to the method for claim 1, it further comprises the side discharging stream partial condensation of compression, the compressed side discharging of generating portion condensation stream thus.
3. according to the method for claim 2, it further comprises makes the compressed side discharging stream of partial condensation return to rectifying section.
4. according to the method for claim 1, it further comprises makes cooling compressed side discharging stream return to rectifying section.
5. according to the method for claim 4, wherein make cooling compressed side discharging stream enter below discharge port.
6. according to the process of claim 1 wherein, side discharging stream is taken out with having in the immediate column plate of column plate of the every column plate of maximum temperature gradient from rectifying section.
7. according to the process of claim 1 wherein, side discharging stream is taken out from lower part of rectifying section.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US35986910P | 2010-06-30 | 2010-06-30 | |
| US61/359,869 | 2010-06-30 | ||
| PCT/US2011/042281 WO2012012153A2 (en) | 2010-06-30 | 2011-06-29 | Improved heat pump distillation for <50% light component in feed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102959051A CN102959051A (en) | 2013-03-06 |
| CN102959051B true CN102959051B (en) | 2014-11-12 |
Family
ID=45398672
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201180029142.5A Active CN102959051B (en) | 2010-06-30 | 2011-06-29 | Improved heat pump distillation for <50% light component in feed |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US20120000244A1 (en) |
| CN (1) | CN102959051B (en) |
| WO (1) | WO2012012153A2 (en) |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102660315B (en) * | 2012-04-12 | 2015-04-01 | 中国寰球工程公司 | Device for controlling endpoint of gasoline blending component extracted from tower sideline vapor phase and method thereof |
| US9937437B2 (en) * | 2013-08-23 | 2018-04-10 | Uop Llc | Fractionation system having rectifying and stripping columns in a single vessel with a uniform diameter |
| US10214695B2 (en) * | 2013-10-16 | 2019-02-26 | Uop Llc | Process for recovering heat from a hydrocarbon separation |
| JP6289112B2 (en) | 2014-01-17 | 2018-03-07 | 東洋エンジニアリング株式会社 | Distillation tower |
| CN104841152A (en) * | 2015-03-26 | 2015-08-19 | 南京炼油厂有限责任公司 | Heat pump-type thermal self-circulation rectification process |
| CN105588472B (en) * | 2016-03-08 | 2018-01-12 | 北京国电龙源环保工程有限公司 | The distribution method of the Load Distribution device of steam Direct Contact Heating method piece-rate system |
| NO342899B1 (en) * | 2016-07-01 | 2018-08-27 | Kanfa Ingenium Process As | System adapted for heating a mixed hydrocarbon wellstream and a method for heating a mixed hydrocarbon wellstream |
| SG11201901967VA (en) | 2016-09-07 | 2019-04-29 | Sabic Global Technologies Bv | System and method for separation of propylene and propane |
| CN110741067B (en) * | 2017-06-08 | 2022-04-12 | 株式会社Lg化学 | Distillation apparatus and distillation method |
| JP7420953B2 (en) * | 2020-01-23 | 2024-01-23 | エボニック オペレーションズ ゲーエムベーハー | Energy-efficient production method for sodium and potassium alkoxides |
| US11643378B2 (en) * | 2021-04-01 | 2023-05-09 | Uop Llc | Propane separation with compressor reboiler |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1179291A (en) * | 1981-10-30 | 1984-12-11 | David T. Ahlberg | Distillation apparatus |
| US5124004A (en) * | 1983-08-22 | 1992-06-23 | Trustees Of Dartmouth College | Distillation process for ethanol |
| US5970743A (en) * | 1998-06-10 | 1999-10-26 | Air Products And Chemicals, Inc. | Production of argon from a cryogenic air separation process |
| US6250106B1 (en) * | 1999-12-13 | 2001-06-26 | Air Products And Chemicals, Inc. | Process for separation of multicomponent fluids using a multizone distallation column |
| US7069743B2 (en) * | 2002-02-20 | 2006-07-04 | Eric Prim | System and method for recovery of C2+ hydrocarbons contained in liquefied natural gas |
| US20040167355A1 (en) * | 2003-02-20 | 2004-08-26 | Abazajian Armen N. | Hydrocarbon products and methods of preparing hydrocarbon products |
| CN100551885C (en) * | 2005-09-29 | 2009-10-21 | 中国石油化工集团公司 | From the product gas of preparation alkene, reclaim the method for low-carbon alkene |
| US8002952B2 (en) * | 2007-11-02 | 2011-08-23 | Uop Llc | Heat pump distillation |
| US7981256B2 (en) * | 2007-11-09 | 2011-07-19 | Uop Llc | Splitter with multi-stage heat pump compressor and inter-reboiler |
| US8182654B2 (en) * | 2008-10-27 | 2012-05-22 | Uop Llc | Heat pump for high purity bottom product |
-
2011
- 2011-06-02 US US13/151,822 patent/US20120000244A1/en not_active Abandoned
- 2011-06-29 WO PCT/US2011/042281 patent/WO2012012153A2/en active Application Filing
- 2011-06-29 CN CN201180029142.5A patent/CN102959051B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102959051A (en) | 2013-03-06 |
| WO2012012153A2 (en) | 2012-01-26 |
| US20120000244A1 (en) | 2012-01-05 |
| WO2012012153A3 (en) | 2012-04-19 |
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